EP0561889B1 - Process for the removal of sulphur compounds from gases - Google Patents
Process for the removal of sulphur compounds from gases Download PDFInfo
- Publication number
- EP0561889B1 EP0561889B1 EP92900559A EP92900559A EP0561889B1 EP 0561889 B1 EP0561889 B1 EP 0561889B1 EP 92900559 A EP92900559 A EP 92900559A EP 92900559 A EP92900559 A EP 92900559A EP 0561889 B1 EP0561889 B1 EP 0561889B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- sulphur
- aqueous solution
- sulphide
- compounds
- concentration
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
- C12M47/18—Gas cleaning, e.g. scrubbers; Separation of different gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/507—Sulfur oxides by treating the gases with other liquids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—Hydrogen sulfide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/84—Biological processes
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
- C01B17/05—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by wet processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
- C02F3/345—Biological treatment of water, waste water, or sewage characterised by the microorganisms used for biological oxidation or reduction of sulfur compounds
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M21/00—Bioreactors or fermenters specially adapted for specific uses
- C12M21/04—Bioreactors or fermenters specially adapted for specific uses for producing gas, e.g. biogas
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S423/00—Chemistry of inorganic compounds
- Y10S423/09—Reaction techniques
- Y10S423/17—Microbiological reactions
Definitions
- the invention relates to a process for the removal of sulphur compounds from a gas flow, in particular from biogas, wherein the gas is washed with an aqueous washing liquid and the spent washing liquid is treated with oxygen and is subsequently reused as a washing liquid.
- H2S Hydrogen sulphide
- Sulphur dioxide is another noxious sulphur compound that is present in gas flows resulting from the combustion of fossil fuels.
- Other harmful sulphur compounds that may be present in gas flows include sulphur trioxide, carbon disulfide, lower alkyl mercaptans etc. Gaseous effluents containing these sulphur compounds must therefore be purified, before they can be discharged into the atmosphere.
- a process for removal of H2S from a gas flow by scrubbing with a washing liquid and subsequently oxidising the absorbed sulphide is known from European patent application EP-A-0 229,587. According to that process, sulphide absorbed in the washing liquid is oxidised non-biologically, in the presence of a catalyst, to products including elemental sulphur which is separated from the system.
- loss of catalyst occurs in such a process, which is an environmental drawback and which increases costs.
- the known process is also relatively expensive because oxidation takes place using pressure.
- a process frequently used is washing biogas with an aqueous liquid having an increased pH, typically a pH of about 11. This increased pH may be adjusted by the addition of sodium hydroxide or other alkalis.
- Such processes are known for example from European patent application EP-A-0 229,587.
- a drawback of scrubbers of this type is their high consumption of chemicals, resulting in relatively high operational costs.
- the price of sodium hydroxide has been increasing strongly recently as a result of a reduced production of chlorine. For many industries, savings in sodium hydroxide will therefore become important.
- Another disadvantage of this process is that it results in an aqueous effluent contaminated with sulphide. According to NL-A-8801009 spent washing liquid from H2S removal from gases can be regenerated by subjecting it to sulphur-oxidising bacteria in the presence of oxygen.
- Another method consists in mixing the biogas with air or oxygen and then conveying it into an oxidation reactor, wherein the sulphide is converted to sulphur, as is known from European patent application EP-A-0 224,889.
- a drawback of this method is that the reactor becomes rather expensive, because the mixture of biogas and oxygen is explosive, requiring safety precautions.
- the reactor should also be rather large because the conversion rate is strongly reduced by the low concentration of oxygen which is allowed ion connection with the gas effluent requirements (explosion standards).
- the invention provides an integrated process for the removal of sulphur compounds, such as H2S and SO2, from gaseous effluents, wherein chemical scrubbing and biological oxidation are combined.
- the process results in an effective purification without the need to continuously add alkali or other chemicals to the washing liquid or to add oxygen to the gas flow and without danger of explosion.
- the first step of the process according to the invention consists in contacting the gaseous effluent with an aqueous washing liquid. This step can be perfomed in a gas scrubber which ensures an effective contact between the gas flow and the washing liquid.
- the washing liquid is buffered at a pH between 6.0 and 9.0, depending on the nature of the gas flow to be treated and especially on the nature of the sulphur compounds to be removed.
- the buffering compounds must be tolerated by the bacteria present in the oxidation reactor.
- Preferred buffering compounds are carbonates, bicarbonates, phosphates and mixtures thereof, especially sodium carbonate and/or sodium bicarbonate.
- the concentration of the buffering compounds depends on the nature of the gas flow, and is generally adjusted to a value within the range of 20 to 2000 meq/l. When sodium carbonate is the buffering compound, its concentration is preferably adjusted to about 1 to 70 g/l. Where in this specification reference is made to bicarbonate and carbonate concentrations, these are expressed as the concentration by weight of HCO3 ⁇ and CO3 ⁇ ions respectively.
- buffering compounds can be done after the washing liquid has left the gas scrubber, but also before it is fed into the scrubber.
- the buffering compound can advantageously be added in the form of carbon dioxide, for example in the gas scrubbing step, when the gaseous effluent contains high levels of carbon dioxide.
- Known autotrophic aerobic cultures such as cultures of the genera Thiobacillus and Thiomicrospira , can be used as bacteria oxidising sulphide to elemental sulphur (herein referred to as sulphide-oxidising bacteria) in the treatment of spent washing liquid in the presence of oxygen in step c).
- the amount of oxygen fed into the washing liquid in the oxidation reactor is adjusted in such a way that the oxidation of the absorbed sulphide predominantly leads to the production of elemental sulphur.
- Such a process for the controlled oxidation of sulphur-containing waste water is described in the mentioned patent application NL-A-8801009.
- the production of sulphur in the oxidation reactor will result in a sulphur slurry which is drawn off.
- the sulphur from this slurry is separated and processed by drying and optionally pruifying, and utilised.
- the sulphur concentration in the washing liquid is generally kept between 0.1 and 50 g/l, preferably between 1 and 50, and more preferably between 10 and 50 g/l (1-5 % by weight).
- the sulphur separation rate is adjusted such that the washing liquid is recycled to the largest extent possible.
- the liquid recovered after processing of the separated sulphur can be returned to the washing liquid.
- H2S or other reduced volatile sulphur compounds such as lower alkyl meraptans or carbon disulphide
- the spent washing liquid containing the sulphur compounds can be directly fed into the reactor containing the sulphide-oxidising bacteria.
- reduced sulphur compounds when dissolved, are referred to herein as "sulphide”, but this term will be understood to include other reduced sulphur species such as dissolved hydrogen sulphide (H2S or HS ⁇ ), disulphide, polysulphides, thiocarbonates, alkanethiolates, etc.
- the pH in the system is preferably kept at about 8-9, particularly at about 8.5.
- the pH is lower, the H2S scrubbing efficiency is insufficient, whereas a higher pH inhibits the activity of most of the bacteria.
- an alkaline washing liquid will be used, or alkali will be added in the initial stage of the process. It was found surprisingly that, after an initial period, no alkali needs to be added any more, in particular when the gas flow also contains carbon dioxide such as in biogas.
- composition of the washing liquid is determined by:
- the level of CO2 absorption is much higher than in a scrubber as operated according to the present invention.
- the total amount of CO2 absorbed depends on the CO2 content of the gas flow, the pH of the scrubbing liquid and the gas flow conducted through the scrubber.
- the CO2 saturation value i.e. the HCO3 ⁇ and CO3 ⁇ concentration
- the CO2 saturation value is not reached, because of the high pH and the short contact time between gas and washing liquid.
- the carbonate and bicarbonate concentrations of the washing liquid will be equal to or close to the saturation level, because of the relatively low pH (and thus the relatively low saturation value, which is about 3-5 g/l for HCO3 ⁇ and about 0.1-0.3 g/l for CO3 ⁇ at pH 8.5) and low gas/liquid flow ratio, and because the system is cyclic.
- the washing liquid will no longer absorb CO2 and no more or very little alkali will be needed for neutralising the CO2.
- the CO2 which is stripped in the oxidation step can be replenished in the absorption step.
- CO2 or (bi)carbonate may be added, preferably to a level of 100-1500, more preferably 200-1200, and most preferably between 400 and 1200 meq/l.
- sulphide oxidation As a result of the oxidation of sulphide with oxygen the concentration of sulphide in the washing liquid will not increase. The sulphur content in the liquid will increase instead, according to the following reactions, which illustrate why the pH of the washing liquid does not decrease.
- the sulphide concentration in the spent washing liquid having a pH of about 8.5 will normally be about 80-100 mg/l, expressed as sulphur. This is a lower concentration than the concentration that is obtained in a conventional H2S scrubber operating at a pH of 10 to 11. Therefore, the scrubber will have to be larger than a conventional scrubber and a higher water/gas flow ratio will be used, for example a water flow to gas flow ratio of 0.1 to 0.2.
- a sulphur concentration of 0.1-50 g/l, in particular 1-50 g/l in the washing liquid improves the removal of H2S from the biogas, while at the same time an effective sulphur separation is ensured.
- the improved H2S removal results from polysulphide production according to the reaction: HS ⁇ + S n ⁇ HS (n+1) ⁇ which causes the absorption equilibrium to shift towards increased absorption.
- a sulphide concentration of 90 mg/l in the spent washing liquid at least half of the sulphide will be bound as polysulphide.
- the present process has the advantage that neutralising agents are not necessary to lower the pH after the scrubber, and therefore no salts are built up in the recirculating washing liquid.
- gaseous effluent contains appreciable levels of sulphur compounds having higher oxidation states, particularly sulphur dioxide, but also sulphur trioxide or other oxidised sulphur compounds, an additional process step is required to reduce the sulphur compounds to sulphide.
- sulphite sulphur compounds having higher oxidation states, when dissolved, are referred to herein as "sulphite", but this term will be understood to include other oxidised species such as dissolved sulphur dioxide, hydrogen sulphite (bisulphite), sulphate, thiosulphate, etc.
- Suitable bacteria for use in the anaerobic reactor to reduce sulphite to sulphide include bacteria reducing sulphur comnpounds (herein reffered to as sulphur-reducing bacteria) such as species of the genera Desulfovibrio , Desulfotomaculum , Desulfomonas , Desulfobulbus , Desulfobacter , Desulfococcus , Desulfonema , Desulfosarcina , Desulfobacterium and Desulfuromas .
- these bacteria are available from various anaerobic cultures and/or grow spontaneously in the anaerobic reactors.
- the pH of the washing liquid is preferably maintained at a level of about 6 to 7. This is higher than in conventional SO2 scrubbers in processes wherein the sulphur dioxide is fixed as gypsum, which typically use a pH below 5.8. This increased pH results in a more efficient SO2 scrubbing.
- the pH may be adjusted by the addition of buffering agents. Preferably, carbonate or bicarbonate is added to a level of 20-100 meq/l, for example about 30 meq/l.
- the washing liquid may be conducted through the scrubber several times before being regenerated.
- the (bi)carbonate concentration of the washing liquid is preferably higher, e.g. 50-200 meq/l.
- the presence of sulphur in the washing liquid was also found to be advantageous. Reaction of sulphur with SO2 (or with HSO3 ⁇ ) results in thiosulphate formation. In the absence of sulphur, SO2 may be further oxidised to sulphate by the oxygen which is often present in combustion gases as well. As sulphate requires more reduction equivalents (electron donor) than thiosulphate does, less electron donor (such as alcohol) is required in the reduction reactor as a result of the presence of sulphur in the washing liquid. In addition, the absorption capacity of the washing liquid is increased by the conversion to thiosulphate.
- the sulphur level is between 0.1 and 50 g/l, preferably between 1 and 50, and most preferably between 10 and 50 g/l.
- H2S and other reduced sulphur compounds such as lower alkyl mercaptans
- Biogas contaminated with H2S (1) enters the scrubber (2) at the bottom and is treated with washing liquid (9).
- Purified gas (3) leaves the reactor at the top.
- the washing liquid (10) which is now contaminated with sulphide leaves the reactor at the bottom and is fed into the oxidation reactor (5), where sulphide is converted to sulphur by the bacteria present therein and oxygen.
- the reactor is supplied with oxygen by an aeration device (4).
- Spent air (6) will have to be treated in a compost filter (7) because of its stench.
- the treated air (8) can be discharged without problems.
- sulphur will result in a sulphur slurry (11) which is partially drawn off.
- the sulphur (12) from this slurry can be dried and utilised.
- the separated aqueous solution (13) is recycled as much as possible in order to save nutrients and alkalinity. If necessary, alkali may be added to flow (9).
- the combustion gas containing SO2 (14) enters the scrubber (2) in a similar way.
- the washing liquid (15) containing sulphite is fed into the reduction reactor (16) wherein sulphite is converted to sulphide by anaerobic bacteria.
- a part of the spent washing liquid may be directly returned to the washing liquid (9) by a short-cut (17).
- the reduced washing liquid (18) is then treated in the oxidation reactor (5) as in the process of figure 1.
- An electron donor, e.g. alcohol, is added through (19).
- Fresh carbonate solution may be added through (19) or elsewhere in the cycle.
- Any gaseous effluent that can be treated with an alkali scrubber can also be purified with the process described herein, provided that the temperature is not too high for the biological activity.
- the process according to the invention is therefore not restricted to biogas. It can also be used for treating combustion gases and ventilation air; in the latter case a phosphate buffer having a concentration of about 50 g/l is preferred.
- the oxidation reactor (5) is a "fixed-film” reactor or a "trickling filter” and contains about 6 m3 of carrier material having a surface area of 200 m2/m3.
- the dimensions of the scrubber (2) are (diameter x height) 0.5 x 2.5 m.
- the reactor is filled with Bionet 200 rings (NSW company).
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Organic Chemistry (AREA)
- Biomedical Technology (AREA)
- Environmental & Geological Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Bioinformatics & Cheminformatics (AREA)
- Zoology (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- Microbiology (AREA)
- Molecular Biology (AREA)
- Genetics & Genomics (AREA)
- Biotechnology (AREA)
- General Health & Medical Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Biochemistry (AREA)
- Sustainable Development (AREA)
- Biodiversity & Conservation Biology (AREA)
- Hydrology & Water Resources (AREA)
- Water Supply & Treatment (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
- Transition And Organic Metals Composition Catalysts For Addition Polymerization (AREA)
Abstract
Description
- The invention relates to a process for the removal of sulphur compounds from a gas flow, in particular from biogas, wherein the gas is washed with an aqueous washing liquid and the spent washing liquid is treated with oxygen and is subsequently reused as a washing liquid.
- The presence of sulphur compounds in gas flows is undesirable, because of their toxicity and their smell. Hydrogen sulphide (H₂S) is a harmful compound that is frequently present in gas flows, especially in biogas originating from anaerobic waste treatment. Sulphur dioxide is another noxious sulphur compound that is present in gas flows resulting from the combustion of fossil fuels. Other harmful sulphur compounds that may be present in gas flows include sulphur trioxide, carbon disulfide, lower alkyl mercaptans etc. Gaseous effluents containing these sulphur compounds must therefore be purified, before they can be discharged into the atmosphere.
- A process for removal of H₂S from a gas flow by scrubbing with a washing liquid and subsequently oxidising the absorbed sulphide is known from European patent application EP-A-0 229,587. According to that process, sulphide absorbed in the washing liquid is oxidised non-biologically, in the presence of a catalyst, to products including elemental sulphur which is separated from the system. However, loss of catalyst occurs in such a process, which is an environmental drawback and which increases costs. The known process is also relatively expensive because oxidation takes place using pressure.
- A process frequently used is washing biogas with an aqueous liquid having an increased pH, typically a pH of about 11. This increased pH may be adjusted by the addition of sodium hydroxide or other alkalis. Such processes are known for example from European patent application EP-A-0 229,587. A drawback of scrubbers of this type is their high consumption of chemicals, resulting in relatively high operational costs. The price of sodium hydroxide has been increasing strongly recently as a result of a reduced production of chlorine. For many industries, savings in sodium hydroxide will therefore become important. Another disadvantage of this process is that it results in an aqueous effluent contaminated with sulphide. According to NL-A-8801009 spent washing liquid from H₂S removal from gases can be regenerated by subjecting it to sulphur-oxidising bacteria in the presence of oxygen.
- Another method consists in mixing the biogas with air or oxygen and then conveying it into an oxidation reactor, wherein the sulphide is converted to sulphur, as is known from European patent application EP-A-0 224,889. A drawback of this method is that the reactor becomes rather expensive, because the mixture of biogas and oxygen is explosive, requiring safety precautions. The reactor should also be rather large because the conversion rate is strongly reduced by the low concentration of oxygen which is allowed ion connection with the gas effluent requirements (explosion standards).
- Known processes for the removal of sulphur dioxide from gaseous effluents involve washing the gas flow with an acidic aqueous washing liquid having a pH which is typically below 5.8. The dissolved SO₂ is usually oxidised and separated as calcium sulphate (gypsum).
- The invention provides an integrated process for the removal of sulphur compounds, such as H₂S and SO₂, from gaseous effluents, wherein chemical scrubbing and biological oxidation are combined. The process results in an effective purification without the need to continuously add alkali or other chemicals to the washing liquid or to add oxygen to the gas flow and without danger of explosion.
- In the process of the invention the following steps are carried out:
- a) contacting the gaseous effluent with an aqueous solution wherein sulphur compounds are dissolved;
- b) adjusting the concentration of buffering compounds such as carbonate and/or bicarbonate and/or phosphate in the aqueous solution to a value between 20 and 2000 meq/l and adjusting the pH of the aqueous solution to between 6 and 9 throughout the process;
- c) subjecting the aqueous solution containing sulphide to sulphide-oxidising bacteria in the presence of oxygen in a reactor wherein sulphide is oxidised to elemental sulphur and hydroxide;
- d) separating elemental sulphur form the aqueous solution; and causing the aqueous solution to contain 0.1 - 50 g of elemental sulphur per liter; and
- e) recycling the aqueous solution to step a).
- The first step of the process according to the invention consists in contacting the gaseous effluent with an aqueous washing liquid. This step can be perfomed in a gas scrubber which ensures an effective contact between the gas flow and the washing liquid.
- An important feature of the present process is that the washing liquid is buffered at a pH between 6.0 and 9.0, depending on the nature of the gas flow to be treated and especially on the nature of the sulphur compounds to be removed. The buffering compounds must be tolerated by the bacteria present in the oxidation reactor. Preferred buffering compounds are carbonates, bicarbonates, phosphates and mixtures thereof, especially sodium carbonate and/or sodium bicarbonate. The concentration of the buffering compounds depends on the nature of the gas flow, and is generally adjusted to a value within the range of 20 to 2000 meq/l. When sodium carbonate is the buffering compound, its concentration is preferably adjusted to about 1 to 70 g/l. Where in this specification reference is made to bicarbonate and carbonate concentrations, these are expressed as the concentration by weight of HCO₃⁻ and CO3⁻⁻ ions respectively.
- Addition of buffering compounds can be done after the washing liquid has left the gas scrubber, but also before it is fed into the scrubber. In case of carbonate/bicarbonate, the buffering compound can advantageously be added in the form of carbon dioxide, for example in the gas scrubbing step, when the gaseous effluent contains high levels of carbon dioxide.
- Known autotrophic aerobic cultures, such as cultures of the genera Thiobacillus and Thiomicrospira, can be used as bacteria oxidising sulphide to elemental sulphur (herein referred to as sulphide-oxidising bacteria) in the treatment of spent washing liquid in the presence of oxygen in step c).
- The amount of oxygen fed into the washing liquid in the oxidation reactor is adjusted in such a way that the oxidation of the absorbed sulphide predominantly leads to the production of elemental sulphur. Such a process for the controlled oxidation of sulphur-containing waste water is described in the mentioned patent application NL-A-8801009.
- The production of sulphur in the oxidation reactor will result in a sulphur slurry which is drawn off. The sulphur from this slurry is separated and processed by drying and optionally pruifying, and utilised.
- It has been found to be advantageous when not all sulphur is drawn off, and thus the separation is carried out discontinuously or partially, resulting in a washing liquid still containing sulphur. The sulphur concentration in the washing liquid is generally kept between 0.1 and 50 g/l, preferably between 1 and 50, and more preferably between 10 and 50 g/l (1-5 % by weight). In particular, the sulphur separation rate is adjusted such that the washing liquid is recycled to the largest extent possible. The liquid recovered after processing of the separated sulphur can be returned to the washing liquid.
- The advantages of the present process are:
- 1. there is hardly any need for chemicals (sodium hydroxide);
- 2. no catalyst is needed;
- 3. the required equipment is simple;
- 4. energy consumption is low;
- 5. no CO₂ is absorbed (after equilibrium has been established);
- 6. no waste effluent results, the sulphur may be sold.
- Experiments have shown that the high (bi)carbonate concentrations do not negatively affect the bacterial activity.
- When H₂S or other reduced volatile sulphur compounds such as lower alkyl meraptans or carbon disulphide, have to be removed, e.g. from biogas, the spent washing liquid containing the sulphur compounds can be directly fed into the reactor containing the sulphide-oxidising bacteria. These reduced sulphur compounds, when dissolved, are referred to herein as "sulphide", but this term will be understood to include other reduced sulphur species such as dissolved hydrogen sulphide (H₂S or HS⁻), disulphide, polysulphides, thiocarbonates, alkanethiolates, etc.
- The pH in the system is preferably kept at about 8-9, particularly at about 8.5. When the pH is lower, the H₂S scrubbing efficiency is insufficient, whereas a higher pH inhibits the activity of most of the bacteria. At the start of the process according to the invention, an alkaline washing liquid will be used, or alkali will be added in the initial stage of the process. It was found surprisingly that, after an initial period, no alkali needs to be added any more, in particular when the gas flow also contains carbon dioxide such as in biogas.
- The composition of the washing liquid is determined by:
- 1. the pH
- 2. the oxidation of sulphide
- In a conventional scrubber absorbing H₂S and CO₂ at high pH, the level of CO₂ absorption is much higher than in a scrubber as operated according to the present invention. The total amount of CO₂ absorbed depends on the CO₂ content of the gas flow, the pH of the scrubbing liquid and the gas flow conducted through the scrubber. In a conventionally operated scrubber the CO₂ saturation value (i.e. the HCO₃⁻ and CO₃⁻⁻ concentration) is not reached, because of the high pH and the short contact time between gas and washing liquid. In the present process however, the carbonate and bicarbonate concentrations of the washing liquid will be equal to or close to the saturation level, because of the relatively low pH (and thus the relatively low saturation value, which is about 3-5 g/l for HCO₃⁻ and about 0.1-0.3 g/l for CO₃⁻⁻ at pH 8.5) and low gas/liquid flow ratio, and because the system is cyclic.
- After an equilibrium has thus been established, the washing liquid will no longer absorb CO₂ and no more or very little alkali will be needed for neutralising the CO₂. The CO₂ which is stripped in the oxidation step can be replenished in the absorption step.
- When the CO₂ content in the gas is lower, CO₂ or (bi)carbonate may be added, preferably to a level of 100-1500, more preferably 200-1200, and most preferably between 400 and 1200 meq/l.
- As to sulphide oxidation:
As a result of the oxidation of sulphide with oxygen the concentration of sulphide in the washing liquid will not increase. The sulphur content in the liquid will increase instead, according to the following reactions, which illustrate why the pH of the washing liquid does not decrease.
The sulphide concentration in the spent washing liquid having a pH of about 8.5 will normally be about 80-100 mg/l, expressed as sulphur. This is a lower concentration than the concentration that is obtained in a conventional H₂S scrubber operating at a pH of 10 to 11. Therefore, the scrubber will have to be larger than a conventional scrubber and a higher water/gas flow ratio will be used, for example a water flow to gas flow ratio of 0.1 to 0.2. - It was found that a sulphur concentration of 0.1-50 g/l, in particular 1-50 g/l in the washing liquid improves the removal of H₂S from the biogas, while at the same time an effective sulphur separation is ensured. The improved H₂S removal results from polysulphide production according to the reaction: HS⁻ + Sn → HS(n+1)⁻
which causes the absorption equilibrium to shift towards increased absorption. At a sulphide concentration of 90 mg/l in the spent washing liquid, at least half of the sulphide will be bound as polysulphide. - The present process has the advantage that neutralising agents are not necessary to lower the pH after the scrubber, and therefore no salts are built up in the recirculating washing liquid.
- When the gaseous effluent contains appreciable levels of sulphur compounds having higher oxidation states, particularly sulphur dioxide, but also sulphur trioxide or other oxidised sulphur compounds, an additional process step is required to reduce the sulphur compounds to sulphide.
- These sulphur compounds having higher oxidation states, when dissolved, are referred to herein as "sulphite", but this term will be understood to include other oxidised species such as dissolved sulphur dioxide, hydrogen sulphite (bisulphite), sulphate, thiosulphate, etc.
- Reduction of sulphite to sulphide can be performed by chemical means, but preferably a biological reduction is carried out using an anaerobic reactor. Suitable bacteria for use in the anaerobic reactor to reduce sulphite to sulphide include bacteria reducing sulphur comnpounds (herein reffered to as sulphur-reducing bacteria) such as species of the genera Desulfovibrio, Desulfotomaculum, Desulfomonas, Desulfobulbus, Desulfobacter, Desulfococcus, Desulfonema, Desulfosarcina, Desulfobacterium and Desulfuromas. In general, these bacteria are available from various anaerobic cultures and/or grow spontaneously in the anaerobic reactors.
- The pH of the washing liquid is preferably maintained at a level of about 6 to 7. This is higher than in conventional SO₂ scrubbers in processes wherein the sulphur dioxide is fixed as gypsum, which typically use a pH below 5.8. This increased pH results in a more efficient SO₂ scrubbing. The pH may be adjusted by the addition of buffering agents. Preferably, carbonate or bicarbonate is added to a level of 20-100 meq/l, for example about 30 meq/l.
- The washing liquid may be conducted through the scrubber several times before being regenerated. In such a process, the (bi)carbonate concentration of the washing liquid is preferably higher, e.g. 50-200 meq/l.
- When SO₂ is removed from gaseous effluents, the presence of sulphur in the washing liquid was also found to be advantageous. Reaction of sulphur with SO₂ (or with HSO₃⁻) results in thiosulphate formation. In the absence of sulphur, SO₂ may be further oxidised to sulphate by the oxygen which is often present in combustion gases as well. As sulphate requires more reduction equivalents (electron donor) than thiosulphate does, less electron donor (such as alcohol) is required in the reduction reactor as a result of the presence of sulphur in the washing liquid. In addition, the absorption capacity of the washing liquid is increased by the conversion to thiosulphate. The sulphur level is between 0.1 and 50 g/l, preferably between 1 and 50, and most preferably between 10 and 50 g/l.
- The process for removing H₂S and other reduced sulphur compounds such as lower alkyl mercaptans is illustrated with reference to figure 1. Biogas contaminated with H₂S (1) enters the scrubber (2) at the bottom and is treated with washing liquid (9). Purified gas (3) leaves the reactor at the top. The washing liquid (10) which is now contaminated with sulphide leaves the reactor at the bottom and is fed into the oxidation reactor (5), where sulphide is converted to sulphur by the bacteria present therein and oxygen. The reactor is supplied with oxygen by an aeration device (4). Spent air (6) will have to be treated in a compost filter (7) because of its stench. The treated air (8) can be discharged without problems. The production of sulphur will result in a sulphur slurry (11) which is partially drawn off. The sulphur (12) from this slurry can be dried and utilised. The separated aqueous solution (13) is recycled as much as possible in order to save nutrients and alkalinity. If necessary, alkali may be added to flow (9).
- The process for removing SO₂ and other oxidised sulphur compounds is ilustrated with reference to figure 2.
- The combustion gas containing SO₂ (14) enters the scrubber (2) in a similar way. The washing liquid (15) containing sulphite is fed into the reduction reactor (16) wherein sulphite is converted to sulphide by anaerobic bacteria. A part of the spent washing liquid may be directly returned to the washing liquid (9) by a short-cut (17). The reduced washing liquid (18) is then treated in the oxidation reactor (5) as in the process of figure 1. An electron donor, e.g. alcohol, is added through (19). Fresh carbonate solution may be added through (19) or elsewhere in the cycle.
- Any gaseous effluent that can be treated with an alkali scrubber can also be purified with the process described herein, provided that the temperature is not too high for the biological activity. The process according to the invention is therefore not restricted to biogas. It can also be used for treating combustion gases and ventilation air; in the latter case a phosphate buffer having a concentration of about 50 g/l is preferred.
- An operating example for H₂S removal is presented in Table A; numbers in the table correspond with the numbers in the accompanying figure 1.
- The oxidation reactor (5) is a "fixed-film" reactor or a "trickling filter" and contains about 6 m³ of carrier material having a surface area of 200 m²/m³. The dimensions of the scrubber (2) are (diameter x height) 0.5 x 2.5 m. The reactor is filled with Bionet 200 rings (NSW company).
TABLE A flow 1 concentration H₂S 0,8 - 1,0 % 1 concentration CH₄ 79 % 1 concentration CO₂ 20 % 1 flow rate 200 m³/h 3 concentration H₂S 150 ppm 3 concentration CH₄ 79 % 3 concentration CO₂ 20 % 3 flow rate 200 m³/ h 10 sulphide concentration 89 mg/ l 10 bicarbonate concentration 7 g/ l 10 sulphur concentration 3 % 10 pH 8.2 10 flow rate 30 m³/ h 9 sulphide concentration < 5 mg/ l 9 sulphur concentration ca 3 % 9 pH 8.4 9 flow rate 30 m³/h
CO₂ which is present in the (bio)gas will also partially be absorbed in the washing liquid. As a result of the recycling of the washing liquid a carbon dioxide equilibrium will be established according to the following reactions:
H₂O + CO₂ ⇄ H₂CO₃ ⇄ HCO₃⁻ + H⁺ ⇄ CO₃⁻⁻ + 2H⁺
The concentration of the dissolved carbonates produced depends of course on the CO₂ concentration in the gas to be purified. The carbonate concentration is about 4-70 g/l, when the CO₂ concentration in the gas is between 10 and 20%. The process is found to operate particularly effectively at such concentrations. A carbonate concentration of more than 70 g/l is not suitable, since it will adversely affect the activity of the bacteria in the oxidation reactor.
Claims (10)
- Process for the removal of sulphur compounds from a gaseous effluent, comprising the steps of:a) contacting the gaseous effluent with an aqueous solution wherein sulphur compounds are dissolved;c) subjecting the aqueous solution containing sulphide to sulphide-oxidising bacteria in the presence of oxygen in a reactor wherein sulphide is oxidised to elemental sulphur;d) separating elemental sulphur form the aqueous solution; ande) recycling the aqueous solution to step a);characterised in that it further comprises the step of:b) adjusting the concentration of buffering compounds such as carbonate and/or bicarbonate and/or phosphate in the aqueous solution to a value between 20 and 2000 meq/l and adjusting the pH of the aqueous solution to between 6 and 9 throughout the process; and
after step d) causing the aqueous solution to contain 0.1-50 g of elemental sulphur per l. - Process of Claim 1, wherein the gaseous effluent in step a) contains hydrogen sulphide and the concentration of buffering compounds in step b) is adjusted to a value between 100 and 1500 meq/l.
- Process of Claim 2, wherein in step b) the buffering compounds comprise carbonate and/or bicarbonate the concentration of which is adjusted to a value between 200 and 1200 meq/l.
- Process according to any of claims 1-3, wherein the pH of the aqueous solution is adjusted to between 8 and 9.
- Process according to claim 1, wherein the gaseous effluent in step a) contains sulphur dioxide, comprising, after step a) and before step c), the additional step of subjecting the aqueous solution containing the sulphur compounds to a reduction of the sulphur compounds to sulphide.
- Process according to claim 5, wherein the reduction is performed using bacteria reducing sulphur compounds.
- Process according to claim 5 or 6, wherein the concentration of buffering compounds is adjusted to a value between 20 and 200 meq/l.
- Process according to any of claims 1-7, wherein in step a) the gaseous effluent contains carbon dioxide.
- Process according to any of claims 1-8, wherein after step d) the aqueous solution is caused to contain 1-50 g of elemental sulphur per l.
- Process according to claim 9, wherein in step e) the aqueous solution contains 10-50 g of elemental sulphur per l.
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
NL9002661A NL9002661A (en) | 1990-12-04 | 1990-12-04 | PROCESS FOR THE REMOVAL OF H2S FROM GAS. |
NL9002661 | 1990-12-04 | ||
PCT/NL1991/000250 WO1992010270A1 (en) | 1990-12-04 | 1991-12-04 | Process for the removal of sulphur compounds from gases |
Publications (2)
Publication Number | Publication Date |
---|---|
EP0561889A1 EP0561889A1 (en) | 1993-09-29 |
EP0561889B1 true EP0561889B1 (en) | 1994-11-02 |
Family
ID=19858088
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP92900559A Expired - Lifetime EP0561889B1 (en) | 1990-12-04 | 1991-12-04 | Process for the removal of sulphur compounds from gases |
Country Status (22)
Country | Link |
---|---|
US (1) | US5354545A (en) |
EP (1) | EP0561889B1 (en) |
JP (1) | JPH0775655B2 (en) |
KR (1) | KR960010378B1 (en) |
AT (1) | ATE113497T1 (en) |
AU (1) | AU648129B2 (en) |
BG (1) | BG61069B1 (en) |
BR (1) | BR9107117A (en) |
CA (1) | CA2096660C (en) |
CZ (1) | CZ285699B6 (en) |
DE (1) | DE69104997T2 (en) |
DK (1) | DK0561889T3 (en) |
EE (1) | EE02976B1 (en) |
ES (1) | ES2062883T3 (en) |
FI (1) | FI109525B (en) |
HU (1) | HU212908B (en) |
NL (1) | NL9002661A (en) |
NO (1) | NO180325C (en) |
PL (1) | PL168365B1 (en) |
RU (1) | RU2089267C1 (en) |
UA (1) | UA27039C2 (en) |
WO (1) | WO1992010270A1 (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9764966B2 (en) | 2012-12-24 | 2017-09-19 | Paques I.P. B.V. | Hydrogen sulfide removal from anaerobic treatment |
Families Citing this family (72)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
RU2108982C1 (en) * | 1992-05-26 | 1998-04-20 | Паквес Б.В. | Method for recovering sulphur compounds from water (alternatives) and method for cleaning sulphur-laden flue gases |
NL9301000A (en) * | 1993-06-10 | 1995-01-02 | Pacques Bv | Method for the purification of waste water containing sulphide. |
DE69407905T2 (en) * | 1993-09-20 | 1998-04-30 | Babcock & Wilcox Co | Flue gas desulfurization with biological regeneration |
AUPM301993A0 (en) * | 1993-12-17 | 1994-01-20 | Microsystem Controls Pty Ltd | Coin validator |
US5480550A (en) * | 1994-05-05 | 1996-01-02 | Abb Environmental Services, Inc. | Biotreatment process for caustics containing inorganic sulfides |
US5501185A (en) * | 1995-01-06 | 1996-03-26 | Kohler Co. | Biogas-driven generator set |
NL9500577A (en) * | 1995-03-24 | 1996-11-01 | Pacques Bv | Method for cleaning gases. |
US5785888A (en) * | 1995-03-24 | 1998-07-28 | Milmac Operating Company | Method for removal of sulfur dioxide |
CA2253936C (en) * | 1996-05-10 | 2006-01-31 | Paques Bio Systems B.V. | Process for the purification of gases containing hydrogen sulphide |
US6287873B2 (en) | 1996-05-20 | 2001-09-11 | Arctech Inc. | Microbiological desulfurization of sulfur containing gases |
US5981266A (en) * | 1996-05-20 | 1999-11-09 | Gas Research Institute | Microbial process for the mitigation of sulfur compounds from natural gas |
EP0845288A1 (en) * | 1996-11-27 | 1998-06-03 | Thiopaq Sulfur Systems B.V. | Process for biological removal of sulphide |
NL1006339C2 (en) * | 1997-06-17 | 1998-12-21 | Stork Eng & Contractors Bv | Process for desulfurizing waste gases. |
NL1008407C2 (en) * | 1998-02-25 | 1999-08-26 | Hoogovens Tech Services | Gas scrubbing process using an anaerobic reactor to remove sulfur dioxide from the scrubber liquid |
US6306288B1 (en) | 1998-04-17 | 2001-10-23 | Uop Llc | Process for removing sulfur compounds from hydrocarbon streams |
US6287365B1 (en) | 1999-01-13 | 2001-09-11 | Uop Llc | Sulfur production process |
US6120581A (en) * | 1999-01-13 | 2000-09-19 | Uop Llc | Sulfur production process |
US6245553B1 (en) | 1999-08-05 | 2001-06-12 | Gene E. Keyser | Method and apparatus for limiting emissions from a contained vessel |
EP1127850A1 (en) * | 2000-02-25 | 2001-08-29 | Nederlandse Organisatie Voor Toegepast-Natuurwetenschappelijk Onderzoek Tno | Removal of sulfur compounds from wastewater |
US6521201B1 (en) | 2001-02-14 | 2003-02-18 | Uop Llc | Process for recovery of high purity hydrophilic sulfur |
DE10119991A1 (en) * | 2001-04-23 | 2002-10-24 | Stephan Pieper | Purification of biogas containing hydrogen sulfide and ammonia, removes hydrogen sulfide at least partially by absorption into alkaline wash solution |
AT411332B (en) * | 2002-04-04 | 2003-12-29 | Profactor Produktionsforschung | Plant separating hydrogen sulfide from biogas using microorganisms, for use in fuel cells, mixes process fluid with oxidant in reactor |
EP1560801B1 (en) | 2002-11-14 | 2007-05-16 | Shell Internationale Researchmaatschappij B.V. | A process for the manufacture of sulphur-containing ammonium phosphate fertilizers |
US7588627B2 (en) * | 2003-04-17 | 2009-09-15 | Shell Oil Company | Process for the removal of H2S and mercaptans from a gas stream |
DE10340049A1 (en) * | 2003-08-28 | 2005-03-24 | Micropro Gmbh | Microbial process and plant for the purification of gases |
WO2005044742A1 (en) * | 2003-11-11 | 2005-05-19 | Paques B.V. | Process for the biological treatment of sulphur salts |
AR046755A1 (en) | 2003-12-10 | 2005-12-21 | Shell Int Research | SULFUR PELLET INCLUDING A H2S SUPPRESSOR |
EP1720798A2 (en) * | 2004-03-03 | 2006-11-15 | Shell Internationale Research Maatschappij B.V. | A process for the high recovery efficiency of sulfur from an acid gas stream |
BRPI0508284A (en) * | 2004-03-03 | 2007-08-07 | Shell Intenationale Res Mij B | sulfur recovery process |
MY140997A (en) | 2004-07-22 | 2010-02-12 | Shell Int Research | Process for the removal of cos from a synthesis gas stream comprising h2s and cos |
AU2005278126B2 (en) | 2004-08-06 | 2010-08-19 | General Electric Technology Gmbh | Ultra cleaning of combustion gas including the removal of CO2 |
CN100360212C (en) * | 2005-07-21 | 2008-01-09 | 四川大学 | Waste gas control method by removing sulfur dioxide for resource utilization |
EA200801713A1 (en) | 2006-01-18 | 2008-12-30 | Шелл Интернэшнл Рисерч Маатсхаппий Б.В. | METHOD FOR REMOVING CARBONESULFIDE AND HYDROGEN FROM A SYNTHESIS GAS FLOW |
DE102006005066B3 (en) * | 2006-02-03 | 2007-10-18 | Perske, Günter | Apparatus and method for producing biogas from organic matter |
US7531159B2 (en) | 2006-07-26 | 2009-05-12 | National Tank Company | Method for extracting H2S from sour gas |
EP2118657B1 (en) * | 2006-12-29 | 2014-05-21 | Abbott Laboratories | Non-denaturing lysis reagent for use with capture-in-solution immunoassay |
US20080190844A1 (en) * | 2007-02-13 | 2008-08-14 | Richard Alan Haase | Methods, processes and apparatus for biological purification of a gas, liquid or solid; and hydrocarbon fuel from said processes |
CN101801500A (en) | 2007-09-10 | 2010-08-11 | 国际壳牌研究有限公司 | Process for producing purified synthesis gas from synthesis gas comprising trace amounts of sulphur contaminants with a metal-organic framework |
US8182577B2 (en) | 2007-10-22 | 2012-05-22 | Alstom Technology Ltd | Multi-stage CO2 removal system and method for processing a flue gas stream |
US7862788B2 (en) | 2007-12-05 | 2011-01-04 | Alstom Technology Ltd | Promoter enhanced chilled ammonia based system and method for removal of CO2 from flue gas stream |
ES2325758B1 (en) * | 2008-03-14 | 2010-06-24 | Endesa Generacion, S.A | GAS CAPTURE IN LIQUID PHASE. |
US7846240B2 (en) | 2008-10-02 | 2010-12-07 | Alstom Technology Ltd | Chilled ammonia based CO2 capture system with water wash system |
US8404027B2 (en) | 2008-11-04 | 2013-03-26 | Alstom Technology Ltd | Reabsorber for ammonia stripper offgas |
EP2208521A3 (en) * | 2009-01-15 | 2010-10-13 | Universität Duisburg-Essen | Method and assembly for processing process water |
US8292989B2 (en) | 2009-10-30 | 2012-10-23 | Alstom Technology Ltd | Gas stream processing |
AU2010230280B2 (en) * | 2009-03-30 | 2013-08-29 | Shell Internationale Research Maatschappij B.V. | Process for producing a purified synthesis gas stream |
CN101637697B (en) * | 2009-08-03 | 2012-01-11 | 庞金钊 | Biological desulfurization method of smoke |
US8293200B2 (en) | 2009-12-17 | 2012-10-23 | Alstom Technology Ltd | Desulfurization of, and removal of carbon dioxide from, gas mixtures |
EP2386648A1 (en) * | 2010-05-10 | 2011-11-16 | Solvay SA | Process for producing biogas |
CN102371109A (en) * | 2010-08-23 | 2012-03-14 | 北京思践通科技发展有限公司 | Method for removing sulfur from gas containing reductive sulfur |
US8329128B2 (en) | 2011-02-01 | 2012-12-11 | Alstom Technology Ltd | Gas treatment process and system |
DE102011007653A1 (en) | 2011-04-19 | 2012-02-02 | Voith Patent Gmbh | Purification of biogas of hydrogen sulfide, comprises removing washing phase impurities e.g. hydrogen sulfide from gas phase of biogas in scrubber using washing medium, and supplying washing medium containing sulfides to aerobic reactor |
US8568512B2 (en) * | 2011-04-29 | 2013-10-29 | A.R.C. Technologies Corporation | Method and system for methane separation and purification from a biogas |
ES2372509B1 (en) * | 2011-10-18 | 2012-10-30 | Biogás Fuel Cell, S.A. | SYSTEM OF SIMULTANEOUS DEPURATION OF BIOGAS AND INDUSTRIAL RESIDUAL EFFLUENTS THROUGH MICROALGAS AND BACTERIA. |
US9162177B2 (en) | 2012-01-25 | 2015-10-20 | Alstom Technology Ltd | Ammonia capturing by CO2 product liquid in water wash liquid |
US9447996B2 (en) | 2013-01-15 | 2016-09-20 | General Electric Technology Gmbh | Carbon dioxide removal system using absorption refrigeration |
PE20160725A1 (en) * | 2013-09-26 | 2016-08-05 | Paques Ip Bv | A PROCESS TO REMOVE SULFIDE FROM AN AQUEOUS SOLUTION |
US8986640B1 (en) | 2014-01-07 | 2015-03-24 | Alstom Technology Ltd | System and method for recovering ammonia from a chilled ammonia process |
AU2015212801B2 (en) * | 2014-02-03 | 2018-12-06 | Paqell B.V. | A process for the biological conversion of bisulphide into elemental sulphur |
EP2944367A1 (en) | 2014-05-16 | 2015-11-18 | Shell International Research Maatschappij B.V. | Process for reducing the total sulphur content of a gas stream |
US20170173531A1 (en) * | 2014-07-17 | 2017-06-22 | Dcl International Inc. | Methods and systems for total organic carbon removal |
EP3034157A1 (en) * | 2015-02-19 | 2016-06-22 | Paqell B.V. | Process for treating a hydrogen sulphide and mercaptans comprising gas |
FR3045663B1 (en) * | 2015-12-22 | 2019-07-19 | Biogaz Pevele | METHANIZATION UNIT EQUIPPED WITH A "U" -shaped LINEAR DIGESTER WITH INTERNAL THERMAL EXCHANGER |
CN111542662A (en) | 2017-12-29 | 2020-08-14 | 维美德技术有限公司 | Method and system for adjusting S/Na balance of pulp mill |
WO2019229167A1 (en) | 2018-06-01 | 2019-12-05 | Paqell B.V. | Process to convert a sulphur compound |
BR112021000947A2 (en) * | 2018-07-19 | 2021-04-20 | Stora Enso Oyj | process for the treatment of industrial alkaline currents |
KR20210137497A (en) * | 2019-03-21 | 2021-11-17 | 바스프 에스이 | Method for purification of alkanes |
DE102019004689B4 (en) * | 2019-07-03 | 2022-04-21 | Verbio Vereinigte Bioenergie Ag | Process for the recovery of molten sulfur from a gas stream containing hydrogen sulfide |
DE102019004693B4 (en) * | 2019-07-03 | 2022-04-21 | Verbio Vereinigte Bioenergie Ag | Process for the recovery of molten sulfur from a gas stream containing hydrogen sulfide |
CN112428379B (en) * | 2020-11-13 | 2022-04-08 | 山东唐唐家居有限公司 | Multi-layer molded door panel molding device and process thereof |
EP4359112A1 (en) | 2021-06-21 | 2024-05-01 | Paques I.P. B.V. | A process to continuously treat a hydrogen sulphide comprising gas and sulphur reclaiming facilities |
CN116904240B (en) * | 2023-09-13 | 2023-11-28 | 山西德远净能环境科技股份有限公司 | Separation equipment for efficiently removing hydrogen sulfide |
Family Cites Families (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE81347C (en) * | ||||
NL25204C (en) * | ||||
US2138214A (en) * | 1935-07-08 | 1938-11-29 | Standard Oil Co California | Process for the production of precipitated sulphur |
BE786389A (en) * | 1971-07-20 | 1973-01-18 | Inst Francais Du Petrole | PROCESS FOR THE ELIMINATION OF SULFUR DIOXIDE CONTAINED IN INDUSTRIAL GAS |
CA1004028A (en) * | 1972-02-29 | 1977-01-25 | The Mead Corporation | Sulfur recovery system |
DE2547675B2 (en) * | 1975-10-24 | 1978-06-01 | Daimler-Benz Ag, 7000 Stuttgart | Process for the wet cleaning of polluted exhaust air |
JPS5348094A (en) * | 1976-10-15 | 1978-05-01 | Ebara Corp | Removing method for hydrogen sulfide and sulfur dioxide |
GB1557295A (en) * | 1977-07-19 | 1979-12-05 | Davy Powergas Ltd | Removal of sulphur dioxide from gas |
SU711142A1 (en) * | 1978-04-27 | 1980-01-25 | Государственный научно-исследовательский институт цветных металлов "Гинцветмет" | Method of processing sulfur-sulfide material |
US4242448A (en) * | 1979-04-12 | 1980-12-30 | Brown Robert S Iii | Regeneration of scrubber effluent containing sulfate radicals |
US4579727A (en) * | 1984-12-04 | 1986-04-01 | The M. W. Kellogg Company | Oxidative removal of hydrogen sulfide from gas streams |
NL8801009A (en) * | 1988-04-19 | 1989-11-16 | Rijkslandbouwuniversiteit | Oxidative biological removal of sulphide from waste water - using short-fall in oxygen, giving conversion largely to sulphur |
-
1990
- 1990-12-04 NL NL9002661A patent/NL9002661A/en not_active Application Discontinuation
-
1991
- 1991-12-04 RU RU9193046322A patent/RU2089267C1/en active
- 1991-12-04 AT AT92900559T patent/ATE113497T1/en not_active IP Right Cessation
- 1991-12-04 UA UA93004280A patent/UA27039C2/en unknown
- 1991-12-04 EP EP92900559A patent/EP0561889B1/en not_active Expired - Lifetime
- 1991-12-04 PL PL91299374A patent/PL168365B1/en unknown
- 1991-12-04 ES ES92900559T patent/ES2062883T3/en not_active Expired - Lifetime
- 1991-12-04 JP JP4502178A patent/JPH0775655B2/en not_active Expired - Lifetime
- 1991-12-04 CA CA002096660A patent/CA2096660C/en not_active Expired - Lifetime
- 1991-12-04 BR BR919107117A patent/BR9107117A/en not_active IP Right Cessation
- 1991-12-04 WO PCT/NL1991/000250 patent/WO1992010270A1/en active IP Right Grant
- 1991-12-04 US US08/070,336 patent/US5354545A/en not_active Expired - Lifetime
- 1991-12-04 CZ CZ931058A patent/CZ285699B6/en not_active IP Right Cessation
- 1991-12-04 HU HU9301632A patent/HU212908B/en unknown
- 1991-12-04 DK DK92900559.3T patent/DK0561889T3/en active
- 1991-12-04 DE DE69104997T patent/DE69104997T2/en not_active Expired - Lifetime
- 1991-12-04 KR KR1019930701637A patent/KR960010378B1/en not_active IP Right Cessation
- 1991-12-04 AU AU90672/91A patent/AU648129B2/en not_active Expired
-
1993
- 1993-05-28 NO NO931943A patent/NO180325C/en not_active IP Right Cessation
- 1993-06-02 BG BG97844A patent/BG61069B1/en unknown
- 1993-06-03 FI FI932534A patent/FI109525B/en not_active IP Right Cessation
-
1994
- 1994-10-26 EE EE9400294A patent/EE02976B1/en unknown
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9764966B2 (en) | 2012-12-24 | 2017-09-19 | Paques I.P. B.V. | Hydrogen sulfide removal from anaerobic treatment |
Also Published As
Publication number | Publication date |
---|---|
HU212908B (en) | 1996-12-30 |
NL9002661A (en) | 1992-07-01 |
KR960010378B1 (en) | 1996-07-31 |
ES2062883T3 (en) | 1994-12-16 |
HU9301632D0 (en) | 1993-11-29 |
CA2096660A1 (en) | 1992-06-05 |
BG61069B1 (en) | 1996-10-31 |
AU648129B2 (en) | 1994-04-14 |
UA27039C2 (en) | 2000-02-28 |
US5354545A (en) | 1994-10-11 |
HUT64875A (en) | 1994-03-28 |
DE69104997D1 (en) | 1994-12-08 |
ATE113497T1 (en) | 1994-11-15 |
BG97844A (en) | 1994-05-27 |
FI932534A (en) | 1993-07-09 |
EP0561889A1 (en) | 1993-09-29 |
DK0561889T3 (en) | 1994-12-05 |
NO180325C (en) | 1997-04-02 |
RU2089267C1 (en) | 1997-09-10 |
CZ105893A3 (en) | 1994-01-19 |
PL168365B1 (en) | 1996-02-29 |
JPH05507235A (en) | 1993-10-21 |
JPH0775655B2 (en) | 1995-08-16 |
AU9067291A (en) | 1992-07-08 |
DE69104997T2 (en) | 1995-03-23 |
FI109525B (en) | 2002-08-30 |
NO931943L (en) | 1993-05-28 |
WO1992010270A1 (en) | 1992-06-25 |
BR9107117A (en) | 1994-02-22 |
EE02976B1 (en) | 1997-04-15 |
CZ285699B6 (en) | 1999-10-13 |
FI932534A0 (en) | 1993-06-03 |
NO180325B (en) | 1996-12-23 |
NO931943D0 (en) | 1993-05-28 |
CA2096660C (en) | 1999-06-01 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP0561889B1 (en) | Process for the removal of sulphur compounds from gases | |
US5976868A (en) | Process for the treatment of gases | |
US6156205A (en) | Process for the purification of gases containing hydrogen sulphide | |
EP0451922B1 (en) | Process for the removal of sulfur dioxide from waste gas | |
SK1999A3 (en) | Sulphur reducing bacterium and its use in biological desulphurisation processes | |
CN104860474A (en) | Method for carbon sequestration and biological treatment of waste alkali liquid containing sulfur | |
RO111357B1 (en) | Method for the removing of the sulphur compounds from water | |
EP0487705A1 (en) | Process for the removal of hydrogensulphide (h 2?s) from biogas. | |
Janssen et al. | Development of a family of large-scale biothechnological processes to desukphurise industrial gases | |
CA2216461C (en) | Process for the treatment of gases | |
VAN HEERINGEN et al. | Development of a family of large-scale biotechnological processes to desulphurise industrial gasses | |
JPS58122093A (en) | Treatment for waste water containing sodium sulfide and/or sodium hydrosulfide |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
|
17P | Request for examination filed |
Effective date: 19930514 |
|
AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): AT BE CH DE DK ES FR GB GR IT LI LU NL SE |
|
17Q | First examination report despatched |
Effective date: 19940211 |
|
ITF | It: translation for a ep patent filed |
Owner name: DE DOMINICIS & MAYER S.R.L. |
|
GRAA | (expected) grant |
Free format text: ORIGINAL CODE: 0009210 |
|
AK | Designated contracting states |
Kind code of ref document: B1 Designated state(s): AT BE CH DE DK ES FR GB GR IT LI LU NL SE |
|
REF | Corresponds to: |
Ref document number: 113497 Country of ref document: AT Date of ref document: 19941115 Kind code of ref document: T |
|
REG | Reference to a national code |
Ref country code: DK Ref legal event code: T3 |
|
REF | Corresponds to: |
Ref document number: 69104997 Country of ref document: DE Date of ref document: 19941208 |
|
REG | Reference to a national code |
Ref country code: ES Ref legal event code: FG2A Ref document number: 2062883 Country of ref document: ES Kind code of ref document: T3 |
|
ET | Fr: translation filed | ||
REG | Reference to a national code |
Ref country code: GR Ref legal event code: FG4A Free format text: 3014755 |
|
PLBI | Opposition filed |
Free format text: ORIGINAL CODE: 0009260 |
|
26 | Opposition filed |
Opponent name: BIOTHANE SYSTEMS INTERNATIONAL Effective date: 19950727 |
|
NLR1 | Nl: opposition has been filed with the epo |
Opponent name: BIOTHANE SYSTEMS INTERNATIONAL |
|
PLBF | Reply of patent proprietor to notice(s) of opposition |
Free format text: ORIGINAL CODE: EPIDOS OBSO |
|
PLBF | Reply of patent proprietor to notice(s) of opposition |
Free format text: ORIGINAL CODE: EPIDOS OBSO |
|
PLBO | Opposition rejected |
Free format text: ORIGINAL CODE: EPIDOS REJO |
|
PLBN | Opposition rejected |
Free format text: ORIGINAL CODE: 0009273 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: OPPOSITION REJECTED |
|
27O | Opposition rejected |
Effective date: 19961209 |
|
NLR2 | Nl: decision of opposition | ||
REG | Reference to a national code |
Ref country code: GB Ref legal event code: IF02 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: NL Payment date: 20101026 Year of fee payment: 20 Ref country code: FR Payment date: 20110107 Year of fee payment: 20 Ref country code: DK Payment date: 20101227 Year of fee payment: 20 Ref country code: AT Payment date: 20101221 Year of fee payment: 20 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: LU Payment date: 20101224 Year of fee payment: 20 Ref country code: CH Payment date: 20101229 Year of fee payment: 20 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: GR Payment date: 20101221 Year of fee payment: 20 Ref country code: IT Payment date: 20101217 Year of fee payment: 20 Ref country code: SE Payment date: 20101222 Year of fee payment: 20 Ref country code: GB Payment date: 20101224 Year of fee payment: 20 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: DE Payment date: 20110125 Year of fee payment: 20 |
|
PGFP | Annual fee paid to national office [announced via postgrant information from national office to epo] |
Ref country code: BE Payment date: 20101223 Year of fee payment: 20 Ref country code: ES Payment date: 20101221 Year of fee payment: 20 |
|
REG | Reference to a national code |
Ref country code: DE Ref legal event code: R071 Ref document number: 69104997 Country of ref document: DE |
|
REG | Reference to a national code |
Ref country code: DE Ref legal event code: R071 Ref document number: 69104997 Country of ref document: DE |
|
REG | Reference to a national code |
Ref country code: NL Ref legal event code: V4 Effective date: 20111204 |
|
REG | Reference to a national code |
Ref country code: CH Ref legal event code: PL |
|
REG | Reference to a national code |
Ref country code: DK Ref legal event code: EUP |
|
REG | Reference to a national code |
Ref country code: GB Ref legal event code: PE20 Expiry date: 20111203 |
|
BE20 | Be: patent expired |
Owner name: *PAQUES B.V. Effective date: 20111204 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: NL Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION Effective date: 20111204 |
|
REG | Reference to a national code |
Ref country code: SE Ref legal event code: EUG |
|
REG | Reference to a national code |
Ref country code: ES Ref legal event code: FD2A Effective date: 20120220 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: GB Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION Effective date: 20111203 |
|
REG | Reference to a national code |
Ref country code: GR Ref legal event code: MA Ref document number: 950400067 Country of ref document: GR Effective date: 20111205 |
|
REG | Reference to a national code |
Ref country code: AT Ref legal event code: MK07 Ref document number: 113497 Country of ref document: AT Kind code of ref document: T Effective date: 20111204 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: ES Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION Effective date: 20111205 |
|
PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: DE Free format text: LAPSE BECAUSE OF EXPIRATION OF PROTECTION Effective date: 20111205 |